Hydrogen-oxygen heating reaction and gas recovery equipment and method thereof

Abstract

The invention belongs to the technical field of chemical engineering, and particularly relates to hydrogen-oxygen heating reaction and gas recovery equipment and a method thereof. The device comprises a hydrogen input pipeline, an oxygen input pipeline, a hot water output pipeline and a cooling water input pipeline, the application scenes of hydrogen normal-temperature reaction and open-fire-free combustion are expanded, the device is simple in structure, safe, reliable and suitable for large-scale production and application, meanwhile, redundant hydrogen and water vapor generated through reaction can be recycled, and the energy consumption is reduced. The water consumption can be reduced by 5%, the hydrogen recovery efficiency is greater than or equal to 95%, the reaction energy consumption is reduced, and the overall reaction efficiency is improved.

Description

Technical Field

[0001] The present invention belongs to the technical field of chemical engineering, and particularly relates to a hydrogen-oxygen heating reaction and gas recovery device and a method thereof. Background Art

[0002] With the rapid development of the global hydrogen energy industry, the demand for hydrogen production by electrolyzing water has increased significantly, while the oxygen generated simultaneously during electrolyzing water is often ignored, resulting in a waste of energy. Hydrogen and oxygen can achieve a complete reaction on the surface of a catalyst at room temperature, releasing heat, which is a heating method that can achieve fireless operation. However, most current hydrogen-oxygen heating reaction devices mainly recover the water vapor generated by the reaction, and do not recycle the excess hydrogen during the reaction process, resulting in a large amount of energy waste and thus reducing the overall reaction efficiency. Summary of the Invention

[0003] To solve the above technical problems, the present invention provides a hydrogen-oxygen heating reaction and gas recovery device and a method thereof, which can catalytically heat-react hydrogen and oxygen entering the reaction and recycle the excess hydrogen and water vapor. Specifically, in the first aspect of the present invention, a hydrogen-oxygen heating reaction and gas recovery device is provided, including a hydrogen input pipeline, an oxygen input pipeline, a hot water output pipeline, and a cooling water input pipeline. The hydrogen input pipeline and the oxygen input pipeline are both connected to a reactor. A Venturi ejector is provided on the hydrogen input pipeline. The reactor is connected to a condenser through a pipeline. The condensed water in the condenser is connected to the reactor through a pipeline and flows out through the reactor. The condenser is connected to a steam-water separator. The water separated in the steam-water separator is mixed with the condensed water through a pipeline and used as condensed water. The gas separated in the steam-water separator enters a drying tower through a pipeline. The output port of the drying tower is connected to the Venturi ejector through a pipeline.

[0004] In some embodiments, the pressures of the hydrogen input pipeline and the oxygen input pipeline are maintained at 0.1 - 0.2 MPa.

[0005] In some embodiments, the flow rate ratio of hydrogen in the hydrogen input pipeline to oxygen in the oxygen input pipeline is 2:1 - 4:1.

[0006] In some embodiments, the reactor includes an inlet pipe, an outlet pipe, a reactor inner cavity, and a reactor outer cavity connected to the reactor inner cavity. The inlet pipe is connected to the lower part of one side of the reactor inner cavity. The upper part of the other side of the reactor inner cavity is connected to the outlet pipe. The reactor outer cavity is recessed towards the reactor inner cavity to form a flow channel, and the flow channels are evenly distributed in the reactor inner cavity. Every two flow channels form a group, and the flow channels in each group are arranged in a relatively staggered manner and perpendicular to the plane where the inlet pipe is located. The outer wall of the flow channel is connected to a carrier. The reactor outer cavity is provided with a water inlet interface and a water outlet interface.

[0007] In some embodiments, the outer cavity of the reactor is hollow inside to ensure the flow of condensed water, and the intake pipe is connected to the hydrogen input pipe and the oxygen input pipe.

[0008] In some embodiments, there is a flow space between the bottom of the flow channel and the inner wall of the reactor cavity to ensure the flow of gas.

[0009] In some embodiments, a partition plate connected to the outer cavity of the reactor is provided in the flow channel. The partition plate closes the outer cavity of the reactor in the plane where it is located, extends inward into the flow channel, and keeps a distance from the bottom of the flow channel. The partition plate ensures that when condensed water passes through the flow channel, it can only flow through the flow channel.

[0010] In some embodiments, at least one flow channel is vertically connected to the horizontal flow channel, and the horizontal flow channel is externally connected to a horizontal carrier.

[0011] In some embodiments, the carrier and the horizontal carrier are filled with a catalyst. The catalyst is a palladium-activated alumina catalyst with an active concentration ≤ 0.5% and a mass density of 600 - 1200 kg / m 3 。

[0012] The second aspect of the present invention is to provide a method for hydrogen-oxygen heating reaction and gas recovery, which is applicable to hydrogen-oxygen heating reaction and gas recovery equipment. The method includes the following steps: S1. Hydrogen and oxygen enter the reactor and undergo a catalytic reaction through a catalyst; S2. Condensed water first passes through a condenser and then flows into the reactor. Hydrogen and water vapor are cooled by the condenser 103 to form a steam-water mixture, which enters a steam-water separator. The separated water enters the condensed water pipeline for continuous recycling, and the separated gas enters a drying tower for drying; S3. When the gas output from the output port of the drying tower is detected by the gas sampling analyzer AI to have a residual oxygen content < 0.5 ppm and a water content < 1 ppm, the recovered hydrogen enters the suction port of the Venturi ejector and thus re-enters the hydrogen input pipe.

[0013] Beneficial effects: The present invention expands the application scenarios of hydrogen room-temperature reaction and flameless combustion. The device has a simple structure, is safe and reliable, is suitable for large-scale production applications. At the same time, the excess hydrogen and water vapor generated by the reaction can be recycled. The water consumption can be reduced by about 2%, the hydrogen recovery efficiency ≥ 95%, the reaction energy consumption is reduced, and the overall reaction efficiency is improved. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 It is a structural diagram of the equipment of the present invention; Figure 2It is the structure diagram of the reactor in the present invention; Figure 3 It is the partial structure diagram of the reactor in the present invention; Among them, 1. intake pipe; 2. inner cavity of the reactor; 2-1. carrier; 2-2. flow channel; 2-3. horizontal flow channel; 2-4. horizontal carrier; 2-5. partition plate; 3. outer cavity of the reactor; 4. water inlet interface; 5. water outlet interface; 6. exhaust pipe; 101. Venturi ejector; 102. reactor; 103. condenser; 104. steam-water separator; 105. drying tower; 201. valve one; 202. valve two; 203. valve three; 204. valve four; 205. valve five; 301. hydrogen input pipeline; 302. oxygen input pipeline; 303. hot water output pipeline; 304. cooling water input pipeline. Specific embodiments

[0015] Next, the technical solutions of the present invention will be clearly and completely described in conjunction with the accompanying drawings. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments.

[0016] Generally, the components of the embodiments of the present invention described and shown in the drawings here can be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely represents the selected embodiments of the present invention.

[0017] Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.

[0018] In the description of the present invention, it should be noted that the orientation or positional relationship indicated by "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention. In addition, the terms "first", "second", and "third" are only used for descriptive purposes and cannot be understood as indicating or implying relative importance.

[0019] In the description of the present invention, it should be noted that unless otherwise clearly specified and limited, the terms "installation", "connection", and "connection" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific situations.

[0020] As Figure 1 , Figure 2 shown, a hydrogen-oxygen heating reaction and gas recovery device, wherein the hydrogen input pipeline 301 is connected to the gas input port of the reactor 102 through the valve 201 and the Venturi ejector 101; the oxygen input pipeline 302 is connected to the gas input port of the reactor 102 through the valve 202; the output port of the reactor 102 is connected to the condenser 103 through a pipeline; the condenser 103 is provided with a water inlet and a water outlet, the water inlet is provided with a valve 203 and is connected to the cooling water input pipeline 304, and the water outlet is connected to the water inlet interface 4 of the reactor 102; hydrogen and water vapor form a steam-water mixture after being cooled by the condenser 103 and enter the steam-water separator 104; the drain port of the steam-water separator 104 is provided with a valve 204 and is connected to the cooling water input pipeline 304, and the exhaust port is connected to the drying tower 105 through the valve 205; the drying tower 105 is filled with a gas desiccant inside, and hydrogen is transported to the suction port of the Venturi ejector 101 through the valve 206 after being dried from the output port, so as to realize the recycling of hydrogen.

[0021] The gas desiccant is silica gel particles with a particle size of 2-5 mm.

[0022] The medium flow rate transported in the hydrogen input pipeline 301 is controlled by the valve 201, the medium flow rate transported in the oxygen input pipeline 302 is controlled by the valve 202, and the medium flow rate transported in the cooling water input pipeline 304 is controlled by the valve 203.

[0023] The medium flow rate transported from the drain port of the steam-water separator 104 to the cooling water input pipeline is controlled by the valve 204, the medium flow rate transported from the exhaust port of the steam-water separator 104 to the drying tower 105 is controlled by the valve 205, and the medium flow rate transported from the output port of the drying tower 105 to the Venturi ejector 101 is controlled by the valve 206.

[0024] The hydrogen input pipeline 301, the oxygen input pipeline 302 and the cooling water input pipeline 304 are provided with flow sensors FT for detecting gas and liquid flow rates; The reactor 102 is provided with a pressure sensor PT for detecting the internal pressure thereof, and the gas pressures of the valve 201 and the valve 202 are controlled by a pressure regulator PIC; The reactor 102 is provided with a temperature sensor TT for detecting the internal reaction temperature and the temperature of the hot water output pipeline 303.

[0025] The pressures of the hydrogen input pipeline and the oxygen input pipeline are maintained at 0.1-0.2 MPa. Under this pressure, the equipment is safer, and at the same time, a certain pressure of the gas input pipeline is ensured, so that the recycled hydrogen can be reused after passing through the Venturi ejector.

[0026] The hydrogen-oxygen flow ratio in the hydrogen input pipeline and the oxygen input pipeline is 2:1 - 4:1. This flow ratio can ensure the full reaction of hydrogen and oxygen.

[0027] Such as Figure 2 , 3 As shown in the figure, the reactor 102 includes an inlet pipe 1, an outlet pipe 6, a reactor inner cavity 2, and a reactor outer cavity 3 connected to the reactor inner cavity 2. The inlet pipe 1 is connected to the lower part of one side of the reactor inner cavity 3, and the upper part of the other side of the reactor inner cavity 3 is connected to the outlet pipe 6. The reactor outer cavity 3 is recessed towards the reactor inner cavity to form a flow channel 2-2, and the flow channels 2-2 are evenly distributed in the reactor inner cavity 2. Every two flow channels 2-2 form a group, and the flow channels 2-2 in each group are arranged in a relatively staggered manner and are perpendicular to the plane where the inlet pipe 1 is located. The outer wall of the flow channel 2-2 is connected to the carrier 2-1. The reactor outer cavity 3 is provided with a water inlet interface 4 and a water outlet interface 5. The water outlet interface 5 is connected to the hot water output pipeline 303. The water inlet interface 4 is connected to the water outlet of the condenser 103 through a pipeline. The spacing between the flow channels 2-2 in each group is designed according to actual needs.

[0028] By setting the flow channels 2-2 in the reactor and connecting the carrier 2-1 carrying the catalyst thereto, first, the reaction path is extended through the staggered flow channels 2-2, promoting the reaction process. Second, when the reaction occurs on the carrier 2-1, the heat can be quickly taken away by the condensed water in the flow channels 2-2, better realizing heat exchange.

[0029] The inside of the reactor outer cavity 3 is hollow to ensure the flow of condensed water. The inlet pipe 1 is connected to the hydrogen input pipeline 301 and the oxygen input pipeline 302.

[0030] A flow space is provided between the bottom of the flow channel 2-2 and the inner wall of the reactor inner cavity 2 to ensure the flow of gas.

[0031] A partition plate 2-5 connected to the reactor outer cavity 3 is provided in the flow channel 2-2. The partition plate 2-5 closes the reactor outer cavity 3 in the plane where it is located, extends inward into the flow channel 2-2, and keeps a distance from the bottom of the flow channel 2-2. The partition plate 2-5 ensures that when the condensed water passes through the flow channel 2-2, it can only flow through the flow channel.

[0032] At least one flow channel 2-2 is vertically connected to the horizontal flow channel 2-3, and the horizontal flow channel 2-3 is externally connected to the horizontal carrier 2-4. By setting the horizontal flow channel 2-3, the flow path of the gas can be well disrupted, playing a role in mixing the flowing gas, making hydrogen and oxygen mix better and react.

[0033] The material carrier 2-1 and the horizontal material carrier 2-4 are filled with a catalyst, which is an activated alumina palladium catalyst with an active concentration ≤ 0.5% and a mass density of 600 - 1200 kg / m 3 .

[0034] Example The method for hydrogen-oxygen heating reaction and gas recovery of the present invention includes the following steps: S1. Open valve 1 201 and valve 2 202. After hydrogen and oxygen enter the reactor 102, they undergo a catalytic reaction through the catalyst. The pressures of the hydrogen input pipeline 301 and the oxygen input pipeline 302 are maintained at 0.1 MPa. The catalyst is an activated alumina palladium catalyst with an active concentration ≤ 0.5% and a mass density of 600 - 1200 kg / m 3 ; S2. Open valve 3 203 and adjust the flow rate of the cooling water input pipeline 304. The cooling water first passes through the condenser 103 and then flows into the reactor 102, and flows out from the water outlet of the reactor 102. When the temperature inside the reactor 102 > 200 °C and the temperature continues to rise, quickly close valve 1 201 and valve 2 202 to terminate the hydrogen-oxygen heating reaction; S3. After hydrogen and water vapor are cooled by the condenser 103, they form a steam-water mixture and enter the steam-water separator 104. Open valve 4 204, and the separated condensed water enters the cooling water input pipeline 304 for continuous recycling; open valve 5 205 and close valve 6 206, and the separated gas enters the drying tower 105; The recycling of cooling water reduces the water consumption by about 2%; S4. After being dried by the gas desiccant, when the residual oxygen content < 0.5 ppm and the water content < 1 ppm are detected by the gas sampling analyzer AI at the output port of the drying tower 105, open valve 6 206, and the recovered hydrogen enters the suction port of the Venturi ejector 101, and thus enters the hydrogen input pipeline 301 again.

[0035] The hydrogen recovery efficiency is calculated to be about 95% through the recovered hydrogen amount detected by the gas sampling analyzer AI.

[0036] At the same time, the inlet temperature of the condensed water of the present invention is 15 °C, and the temperature in the final hot water output pipeline 303 can reach about 70 °C. And at 70 °C hot water, it can be applied to the application scenarios of actual life such as home heating or bathing.

[0037] Comparative Example It is basically the same as the example, except that the reactor uses a conventional horizontal reactor, but its water temperature can only reach about 60 °C. At the same time, the hydrogen recovery rate is 90%.

[0038] The method and device for hydrogen-oxygen heating reaction and gas recovery of the present invention expand the application scenarios of hydrogen reacting at normal temperature and burning without open flame. The device has a simple structure, is safe and reliable, and is suitable for large-scale production applications. At the same time, the excess hydrogen and water vapor generated by the reaction can be reused, reducing the reaction energy consumption and improving the overall reaction efficiency.

[0039] The above are only the preferred specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution and inventive concept of the present invention, making equivalent substitutions or changes should be covered within the protection scope of the present invention.

Claims

1. A hydrogen-oxygen heating reaction and gas recovery device, comprising a hydrogen input pipeline (301), an oxygen input pipeline (302), a hot water output pipeline (303), and a cooling water input pipeline (304), characterized in that: The hydrogen input pipeline (301) and the oxygen input pipeline (302) are both connected to the reactor (102); a venturi ejector (101) is provided on the hydrogen input pipeline (301); the reactor (102) is connected to a condenser (103) via a pipeline; condensed water in the condenser (103) is connected to the reactor (102) via a pipeline and flows out of the reactor (102); the condenser (103) is connected to a steam-water separator (104); the water separated in the steam-water separator (104) is mixed with condensed water via a pipeline and used as condensed water; the gas separated in the steam-water separator (104) enters a drying tower (105) via a pipeline; and the output port of the drying tower (105) is connected to the venturi ejector (101) via a pipeline.

2. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 1, characterized in that: The pressure of the hydrogen input pipeline (301) and the oxygen input pipeline (302) is maintained at 0.1-0.2 MPa.

3. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 1, characterized in that: The flow ratio of hydrogen in the hydrogen input pipeline (301) and oxygen in the oxygen input pipeline (302) is 2:1-4:

1.

4. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 1, characterized in that: The reactor (102) comprises an air inlet pipe (1), an air outlet pipe (6), a reactor inner cavity (2), and a reactor outer cavity (3) connected to the reactor inner cavity (2); the air inlet pipe (1) is connected to the lower part of one side of the reactor inner cavity (3); the upper part of the other side of the reactor inner cavity (3) is connected to the air outlet pipe (6); the reactor outer cavity (3) is recessed into the reactor inner cavity to form a flow channel (2-2); the flow channels (2-2) are evenly distributed in the reactor inner cavity (2); every two flow channels (2-2) form a group; the flow channels (2-2) in each group are relatively staggered and perpendicular to the plane where the air inlet pipe (1) is located; the outer wall of the flow channel (2-2) is connected to the carrier (2-1); and the reactor outer cavity (3) is provided with a water inlet interface (4) and a water outlet interface (5).

5. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 4, characterized in that: The reactor outer cavity (3) is hollow inside to ensure the flow of condensed water, and the air inlet pipe (1) is connected to the hydrogen input pipeline (301) and the oxygen input pipeline (302).

6. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 4, characterized in that: A flow space is provided between the bottom of the flow channel (2-2) and the inner wall of the reactor cavity (2) to ensure the circulation of gas.

7. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 6, characterized in that: The flow channel (2-2) is provided with a partition plate (2-5) connected to the reactor outer cavity (3); the partition plate (2-5) closes the reactor outer cavity (3) on the plane where it is located, and extends inwardly to the inside of the flow channel (2-2) and maintains a distance from the bottom of the flow channel (2-2); the partition plate (2-5) ensures that when condensed water passes through the flow channel (2-2), it can only flow through the flow channel.

8. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 7, characterized in that: At least one flow channel (2-2) is vertically connected to a horizontal flow channel (2-3), and the horizontal flow channel (2-3) is externally connected to a horizontal carrier (2-4).

9. The hydrogen-oxygen heating reaction and gas recovery equipment according to claim 8, characterized in that: The carrier (2-1) and the horizontal carrier (2-4) are filled with a catalyst, wherein the catalyst is an active aluminum oxide palladium catalyst with an activity concentration of ≤0.5% and a mass density of 600-1200 kg / m 3 .

10. A method for hydrogen-oxygen heating reaction and gas recovery, applicable to the hydrogen-oxygen heating reaction and gas recovery equipment according to any one of claims 1 to 9, characterized in that: The method comprises the following steps: S1, hydrogen and oxygen are introduced into the reactor (102) and then subjected to a catalytic reaction by a catalyst; S2, the condensed water first passes through the condenser (103) and then flows into the reactor (102), the hydrogen and water vapor are cooled in the condenser (103) to form a steam-water mixture and enter the steam-water separator (104), the separated water enters the condensed water pipeline for continuous recycling, and the separated gas enters the drying tower (105) for drying; S3. When the residual oxygen content of the gas output from the outlet of the drying tower (105) is less than 0.5 ppm and the water content is less than 1 ppm as detected by the gas sampling analyzer AI, the recovered hydrogen enters the air intake of the venturi ejector (101) and then enters the hydrogen input pipeline (301) again.

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